CN101560152A - Method for synthesizing propionate - Google Patents
Method for synthesizing propionate Download PDFInfo
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- CN101560152A CN101560152A CNA2009100273135A CN200910027313A CN101560152A CN 101560152 A CN101560152 A CN 101560152A CN A2009100273135 A CNA2009100273135 A CN A2009100273135A CN 200910027313 A CN200910027313 A CN 200910027313A CN 101560152 A CN101560152 A CN 101560152A
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- Prior art keywords
- propionic acid
- reaction
- propionate
- catalyst
- synthesizing
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Links
- 238000000034 method Methods 0.000 title claims abstract description 26
- XBDQKXXYIPTUBI-UHFFFAOYSA-M Propionate Chemical compound CCC([O-])=O XBDQKXXYIPTUBI-UHFFFAOYSA-M 0.000 title claims abstract description 21
- 230000002194 synthesizing effect Effects 0.000 title claims abstract description 20
- XBDQKXXYIPTUBI-UHFFFAOYSA-N dimethylselenoniopropionate Natural products CCC(O)=O XBDQKXXYIPTUBI-UHFFFAOYSA-N 0.000 claims abstract description 108
- 238000006243 chemical reaction Methods 0.000 claims abstract description 55
- 235000019260 propionic acid Nutrition 0.000 claims abstract description 54
- IUVKMZGDUIUOCP-BTNSXGMBSA-N quinbolone Chemical compound O([C@H]1CC[C@H]2[C@H]3[C@@H]([C@]4(C=CC(=O)C=C4CC3)C)CC[C@@]21C)C1=CCCC1 IUVKMZGDUIUOCP-BTNSXGMBSA-N 0.000 claims abstract description 54
- 239000003054 catalyst Substances 0.000 claims abstract description 37
- 150000001336 alkenes Chemical class 0.000 claims abstract description 21
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims abstract description 12
- 239000002253 acid Substances 0.000 claims abstract description 12
- 239000003456 ion exchange resin Substances 0.000 claims abstract description 12
- 229920003303 ion-exchange polymer Polymers 0.000 claims abstract description 12
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical group CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 21
- 239000011347 resin Substances 0.000 claims description 16
- 229920005989 resin Polymers 0.000 claims description 16
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 13
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 13
- JAELLLITIZHOGQ-UHFFFAOYSA-N tert-butyl propanoate Chemical compound CCC(=O)OC(C)(C)C JAELLLITIZHOGQ-UHFFFAOYSA-N 0.000 claims description 11
- IJMWOMHMDSDKGK-UHFFFAOYSA-N Isopropyl propionate Chemical group CCC(=O)OC(C)C IJMWOMHMDSDKGK-UHFFFAOYSA-N 0.000 claims description 10
- 238000007259 addition reaction Methods 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 5
- FKRCODPIKNYEAC-UHFFFAOYSA-N ethyl propionate Chemical compound CCOC(=O)CC FKRCODPIKNYEAC-UHFFFAOYSA-N 0.000 claims description 5
- 239000001257 hydrogen Substances 0.000 claims description 5
- 229910052739 hydrogen Inorganic materials 0.000 claims description 5
- 229920001577 copolymer Polymers 0.000 claims description 4
- -1 isopropyl ester Chemical class 0.000 claims description 4
- 125000001273 sulfonato group Chemical group [O-]S(*)(=O)=O 0.000 claims description 4
- 125000000999 tert-butyl group Chemical group [H]C([H])([H])C(*)(C([H])([H])[H])C([H])([H])[H] 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 2
- 230000035484 reaction time Effects 0.000 claims description 2
- 238000005886 esterification reaction Methods 0.000 abstract description 7
- 239000002351 wastewater Substances 0.000 abstract description 4
- 239000000047 product Substances 0.000 abstract description 3
- 230000015572 biosynthetic process Effects 0.000 abstract description 2
- 239000006227 byproduct Substances 0.000 abstract description 2
- 208000012839 conversion disease Diseases 0.000 abstract description 2
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000002245 particle Substances 0.000 abstract description 2
- 238000003786 synthesis reaction Methods 0.000 abstract description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 2
- 230000009466 transformation Effects 0.000 description 12
- 238000001914 filtration Methods 0.000 description 8
- 238000004587 chromatography analysis Methods 0.000 description 7
- 239000007789 gas Substances 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- WYURNTSHIVDZCO-UHFFFAOYSA-N Tetrahydrofuran Chemical compound C1CCOC1 WYURNTSHIVDZCO-UHFFFAOYSA-N 0.000 description 6
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- 230000032050 esterification Effects 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- XEKOWRVHYACXOJ-UHFFFAOYSA-N Ethyl acetate Chemical compound CCOC(C)=O XEKOWRVHYACXOJ-UHFFFAOYSA-N 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- YLQBMQCUIZJEEH-UHFFFAOYSA-N tetrahydrofuran Natural products C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 3
- 229920000557 Nafion® Polymers 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 150000001733 carboxylic acid esters Chemical class 0.000 description 2
- 239000012159 carrier gas Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- RSWGJHLUYNHPMX-UHFFFAOYSA-N 1,4a-dimethyl-7-propan-2-yl-2,3,4,4b,5,6,10,10a-octahydrophenanthrene-1-carboxylic acid Chemical compound C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 1
- 239000004902 Softening Agent Substances 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- 239000013543 active substance Substances 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 150000007942 carboxylates Chemical class 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000178 monomer Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The invention belongs to the field of propionate synthesis, and discloses a method for synthesizing propionate. The method is that propionic acid and olefin are synthesized into propionate under the action of a macroporous strong-acid ion exchange resin catalyst. The direct addition esterification reaction of propionic acid and olefin belongs to atom economic reaction, the reaction conversion rate is high, the selectivity is high, the byproducts are few, and no wastewater is generated in the whole reaction process. The catalyst has larger particle diameter, is easy to separate from the product, can be recycled, and has important economic benefit and good environmental benefit.
Description
Technical field
The invention belongs to the synthetic field of propionic ester, relate to a kind of method of synthesizing propionate, be specifically related to the method that a kind of propionic acid and propylene react propionic acid synthesized isopropyl ester or the propionic acid and the propionic acid synthesized tert-butyl ester of isobutene reaction.
Background technology
The propionic ester that contains the higly branched chain structure as isopropyl propionate, the propionic acid tert-butyl ester, is the broad-spectrum important Chemicals of a class, can be used as solvent, softening agent, foodstuff additive, tensio-active agent and polymer monomer etc.
The technology of present industrial production carboxylicesters mainly is to be that raw material, sulfuric acid or tosic acid are that catalyzer carries out esterification with carboxylic acid and alcohol, and product separation need pass through processing steps such as neutralization, washing, extraction, rectifying.This acid alcohol esterification process synthesis technique exists that long flow path, equipment corrosion are serious, catalyzer can not reclaim, and problem such as discharge of wastewater is many.
With propionic acid and alkene is raw material direct addition esterification synthesizing propionate, does not have water to generate in reaction process, adopts solid acid catalyst simultaneously, then can simplify technical process, stop discharge of wastewater.And the alcohol that alkene is corresponding with it is compared, and is cheap, reduced the raw materials cost of ester.Therefore, the operational path by propionic acid and alkene direct addition esterification synthesizing carboxylate more and more receives publicity.
BASF AG (patent GB1574501) is a catalyzer with the ion exchange resin of 10～200 microns of particle diameters, a series of sour alkene esterification is generated carboxylicesters study.Per hour 70 parts of propionic acid and per hour 30 parts of propylene under 120 ℃, 23bar condition, react, the transformation efficiency of propionic acid is 70%.Because granules of catalyst is thinner, need to adopt 10 microns metallic filter filtering catalyst.
It is catalyzer that union carbide corporation (patent WO8100846) adopts Dupont company business-like Nafion series Hydrogen perfluorinated sulfonic resin, and propionic acid and iso-butylene are solvent with the tetrahydrofuran (THF), react 6 hours down at 25 ℃, and the propionic acid transformation efficiency is 51%.
Above-mentioned solid resin catalyzer is with respect to liquid acid catalysts such as sulfuric acid, and little to equipment corrosion, catalyzer can be recycled.But the propionic acid transformation efficiency is all lower, and the resin catalyst fine size that BASF AG adopts, catalyst separating difficulty, the perfluor Nafion catalyst series cost height that union carbide corporation adopts, in propionic acid and isobutene reaction, also use a large amount of tetrahydrofuran solvents, reaction product separating energy consumption height.
The technical scheme that do not have as yet at present that cost is low, environmental friendliness, employing large granular catalyst that transformation efficiency is high is used for propionic acid and alkene addition reaction synthesizing propionate is reported.
Summary of the invention
The purpose of this invention is to provide a kind of employing macropore strong acid ion exchange resin is catalyzer, make propionic acid respectively with the method for propylene, the propionic acid synthesized isopropyl ester of iso-butylene addition reaction or the propionic acid tert-butyl ester.
Another object of the present invention provides the application of macropore strong acid ion-exchange resin catalyst in propionic acid and alkene addition reaction synthesizing propionate.
Purpose of the present invention can reach by following measure:
A kind of method of synthesizing propionate, this method are propionic acid and alkene synthesizing propionate under the effect of macropore strong acid ion-exchange resin catalyst.
Described method, wherein alkene is propylene, iso-butylene; Propionic ester is isopropyl propionate, the propionic acid tert-butyl ester.
Described method, wherein the macropore strong acid ion-exchange resin catalyst is the vinylbenzene-styrene copolymer of Hydrogen band sulfonate group, is preferably NKC-9 type resin.This NKC-9 type resin is the commercial prod that Chemical Plant of Nankai Univ. produces, and granularity is 0.4～1.25mm, and this resin belongs to the vinylbenzene-styrene copolymer of Hydrogen band sulfonate group.
Being reflected in the tank reactor of propionic acid and alkene carried out, and in the disposable adding reactor of propionic acid, alkene can feed reactor continuously, also can feed several times, and the mol ratio that feeds alkene total amount and propionic acid is 0.9～2.5: 1, and preferred 1.0～1.5: 1.
Described method, wherein catalyst consumption is 1%～20% of a propionic acid quality, preferred 3～10%.
Described method, wherein temperature of reaction is 20～160 ℃, and reaction pressure is 0.1～3.0MPa, and the reaction times is 1～20h, preferred 4～8h.
Described method, temperature of reaction was 90～160 ℃ when wherein synthesizing propionate was isopropyl propionate, reaction pressure is 0.6～3.0MPa; Temperature of reaction was 20～40 ℃ when synthesizing propionate was the propionic acid tert-butyl ester, and reaction pressure is 0.1～0.5MPa.
The application of macropore strong acid ion-exchange resin catalyst in propionic acid and alkene addition reaction synthesizing propionate.
Described application, wherein propionic acid and alkene addition reaction synthesizing propionate are propionic acid and the propionic acid synthesized isopropyl ester of propylene addition reaction or the propionic acid and the propionic acid synthesized tert-butyl ester of iso-butylene addition; The macropore strong acid ion-exchange resin catalyst is the NKC-9 resin.
Beneficial effect of the present invention:
Propionic acid of the present invention and alkene direct addition esterification belong to atomic economy reaction, (peak rate of conversion among the present invention is near 90% for the reaction conversion ratio height, as embodiment 3,4,7, than the document height), selectivity height, by product lack, entire reaction course does not have waste water and generates.The granules of catalyst diameter is bigger, separates with product easily and catalyzer can reuse, and not only has important economic benefit, and has good benefits in environment.
Embodiment
The invention will be further elaborated by the following examples.
General explanation:
The analysis condition of isopropyl propionate: capillary chromatographic column is the XE-60 capillary column, and fid detector, toluene are internal standard substance, and carrier gas is a high-purity N
2, 180 ℃ of vaporizer temperature, 180 ℃ of sensing chamber's temperature, 90 ℃ of column temperatures.
The analysis condition of the propionic acid tert-butyl ester: capillary chromatographic column is the XE-60 capillary column, fid detector, and toluene is internal standard substance, and ethyl acetate is done internal standard substance, and carrier gas is a high-purity N
2180 ℃ of temperature of vaporization chamber, 180 ℃ of sensing chamber's temperature, column temperature adopts temperature programming, and 70 ℃ of initial temperatures continue 6min, are warming up to 120 ℃ and lasting 1min with 50 ℃/min then, are raised to 150 ℃ with 30 ℃/min again, continue 5min.)
Embodiment 1:
In the 0.3L reactor, add 100g propionic acid and 20g NKC-9 type resin catalyst, temperature of reaction is 160 ℃, and reaction pressure is 0.7MPa, and mixing speed is 800rpm, feeds propylene reaction 4h continuously with 12.8g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the propionic acid transformation efficiency is 75.1%, calculated with propylene, and the isopropyl propionate selectivity is 97.2%.
Embodiment 2:
In the 0.3L reactor, add 100g propionic acid and 5g NKC-9 type resin catalyst, temperature of reaction is 90 ℃, and pressure is 3.0MPa, and mixing speed is 800rpm, feeds propylene reaction 6h continuously with 11.4g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the propionic acid transformation efficiency is 86.3%, calculated with propylene, and the isopropyl propionate selectivity is 97.1%.
Embodiment 3:
In the 1L reactor, add 300g propionic acid and 21g NKC-9 type resin catalyst, temperature of reaction is 110 ℃, reaction pressure 1.2MPa, mixing speed are 800rpm, feed propylene reaction 9h continuously with 28.3g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the propionic acid transformation efficiency is 89.5%, calculated with propylene, and the isopropyl propionate selectivity is 98.8%.
Embodiment 4:
Adopt the catalyst recirculation of embodiment 3 filtered and recycled to use, other conditions are identical with embodiment 3, and catalyst recirculation uses 5 times reaction result as shown in the table.
| Cycle index | 1 | 2 | 3 | 4 | 5 |
| The propionic acid transformation efficiency | 88.4％ | 89.1％ | 87.7％ | 88.5％ | 89.6％ |
| The isopropyl propionate selectivity | 97.8％ | 98.1％ | 98.5％ | 97.6％ | 97.9％ |
Embodiment 5:
In the 0.3L reactor, add 100g propionic acid, the 6g trimethyl carbinol, 151.3g iso-butylene and 1g NKC-9 type resin catalyst, temperature of reaction is 30 ℃, and reaction pressure is 0.5MPa, and mixing speed is 800rpm, reaction 1h.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the propionic acid transformation efficiency is 77.4%, calculated with iso-butylene, and propionic acid tert-butyl ester selectivity is 96.4%.
Embodiment 6:
In the 0.3L reactor, add 100g propionic acid, the 3g trimethyl carbinol and 4g NKC-9 type resin catalyst, temperature of reaction is 40 ℃, and reaction pressure is 0.1MPa, and mixing speed is 800rpm, feeds isobutene reaction 3h continuously with 30.3g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the propionic acid transformation efficiency is 81.9%, calculated with iso-butylene, and propionic acid tert-butyl ester selectivity is 97.2%.
Embodiment 7:
In the 0.3L reactor, add 100g propionic acid, the 4g trimethyl carbinol and 7g NKC-9 type resin catalyst, temperature of reaction is 30 ℃, reaction pressure 0.1MPa, mixing speed are 800rpm, feed isobutene reaction 4h continuously with 37.8g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the transformation efficiency of propionic acid is 89.6%, calculated with iso-butylene, and the selectivity of the propionic acid tert-butyl ester is 95.3%.
Embodiment 8:
In the 1L reactor, add 300g propionic acid, the 22.5g trimethyl carbinol and 15g NKC-9 type resin catalyst, temperature of reaction is 20 ℃, and reaction pressure is 0.2MPa, and mixing speed is 800rpm, feeds isobutene reaction 6h continuously with 56.8g/h speed.After reaction finished, the reaction solution behind the filtering recovering catalyst adopted gas chromatographic analysis, and the transformation efficiency of propionic acid is 87.3%, calculated with iso-butylene, and the selectivity of the propionic acid tert-butyl ester is 95.1%.
Claims (10)
1, a kind of method of synthesizing propionate is characterized in that this method is propionic acid and alkene synthesizing propionate under the effect of macropore strong acid ion-exchange resin catalyst.
2, method according to claim 1 is characterized in that alkene is propylene, iso-butylene; Propionic ester is isopropyl propionate, the propionic acid tert-butyl ester.
3, method according to claim 1 is characterized in that the macropore strong acid ion-exchange resin catalyst is the vinylbenzene-styrene copolymer of Hydrogen band sulfonate group.
4, method according to claim 3, the vinylbenzene-styrene copolymer that it is characterized in that Hydrogen band sulfonate group are NKC-9 type resin.
5, method according to claim 1, the mol ratio that it is characterized in that alkene total amount and propionic acid is 0.9～2.5: 1, preferred 1.0～1.5: 1.
6, method according to claim 1 is characterized in that catalyst consumption is 1%～20% of a propionic acid quality, preferred 3～10%.
7, according to the described method for preparing propionic ester of claim 1, it is characterized in that temperature of reaction is 20～160 ℃, reaction pressure is 0.1～3.0MPa, the reaction times is 1～20h, preferred 4～8h.
8, method according to claim 1, temperature of reaction is 90～160 ℃ when it is characterized in that synthesizing propionate is isopropyl propionate, reaction pressure is 0.6～3.0MPa; Temperature of reaction was 20～40 ℃ when synthesizing propionate was the propionic acid tert-butyl ester, and reaction pressure is 0.1～0.5MPa.
9, the application of macropore strong acid ion-exchange resin catalyst in propionic acid and alkene addition reaction synthesizing propionate.
10, application according to claim 9 is characterized in that propionic acid and alkene addition reaction synthesizing propionate are propionic acid and the propionic acid synthesized isopropyl ester of propylene addition reaction or the propionic acid and the propionic acid synthesized tert-butyl ester of iso-butylene addition; The macropore strong acid ion-exchange resin catalyst is a NKC-9 type resin.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100273135A CN101560152B (en) | 2009-05-27 | 2009-05-27 | Method for synthesizing propionate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100273135A CN101560152B (en) | 2009-05-27 | 2009-05-27 | Method for synthesizing propionate |
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| CN101560152A true CN101560152A (en) | 2009-10-21 |
| CN101560152B CN101560152B (en) | 2012-05-23 |
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| CN2009100273135A Expired - Fee Related CN101560152B (en) | 2009-05-27 | 2009-05-27 | Method for synthesizing propionate |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104761450A (en) * | 2012-12-20 | 2015-07-08 | 常州市松盛香料有限公司 | Preparation method of ethyl propionate |
| CN106316840A (en) * | 2016-08-23 | 2017-01-11 | 深圳市普利凯新材料股份有限公司 | Method for preparing and purifying tertbutyl propionate |
| CN114940648A (en) * | 2022-06-30 | 2022-08-26 | 常州夏青科技有限公司 | Method for preparing mono-tert-butyl malonate by catalysis of strong acid resin |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE69117871T2 (en) * | 1990-10-31 | 1996-11-07 | Daicel Chem | Process for the preparation of a lower alkyl acetate |
| CN100432039C (en) * | 2007-07-11 | 2008-11-12 | 胡先念 | Method for protective preparation of acidic ion exchange resin catalyst for lower fatty acid ester |
-
2009
- 2009-05-27 CN CN2009100273135A patent/CN101560152B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104761450A (en) * | 2012-12-20 | 2015-07-08 | 常州市松盛香料有限公司 | Preparation method of ethyl propionate |
| CN104761450B (en) * | 2012-12-20 | 2016-08-24 | 常州市松盛香料有限公司 | The preparation method of ethyl propionate |
| CN106316840A (en) * | 2016-08-23 | 2017-01-11 | 深圳市普利凯新材料股份有限公司 | Method for preparing and purifying tertbutyl propionate |
| CN114940648A (en) * | 2022-06-30 | 2022-08-26 | 常州夏青科技有限公司 | Method for preparing mono-tert-butyl malonate by catalysis of strong acid resin |
| CN114940648B (en) * | 2022-06-30 | 2023-11-21 | 常州夏青科技有限公司 | Method for preparing malonic acid mono-tert-butyl ester by catalysis of strong acid resin |
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| Publication number | Publication date |
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| CN101560152B (en) | 2012-05-23 |
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